Two stage anaerobic digestion with intermediate hydrolysis

ABSTRACT

In a system and process, sludge is treated by two stages of anaerobic digestion in series separated by intermediate thickening and hydrolysis. The hydrolysis product is transferred to the second digester essentially without dilution.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation of U.S. application Ser. No.15/671,704, filed Aug. 8, 2017, which is a non-provisional applicationof U.S. Application Ser. No. 62/377,946, filed Aug. 22, 2016. U.S.application Ser. No. 15/671,704 and 62/377,946 are incorporated byreference.

FIELD

This specification relates to treating waste sewage sludge and anaerobicdigestion.

BACKGROUND

A typical wastewater treatment plant (WWTP) produces one or more sewagesludges such as primary sludge and waste activated sludge. Some or allof the sewage sludge may be thickened up to about 6 wt % dried solids.The sewage sludge can be further treated in a mesophilic anaerobicdigester. The resulting digestate is a Class B biosolid with no value orlimited value.

Thermal hydrolysis is most commonly used in commercial anaerobicdigesters according to the CAMBITHP process. In the typical form of thisprocess, waste sludge is hydrolysed by a combination of heat (about 160degrees C.) and pressure (at least several atmospheres) prior toanaerobic digestion. Because the viscosity of the waste sludge isreduced in the process, the waste sludge may be thickened, for exampleto about 8-16% dried solids by weight (DS) before hydrolysis. Theanaerobic digester then operates at about 4-6% DS in the digestercompared to 2-3% DS for a conventional digester coupled to a WWTP.

International Publication Numbers WO 2014/137218 and WO 2016/066752 giveexamples of the use of thermal hydrolysis devices in combination withanaerobic digesters.

Introduction to the Invention

When thermal hydrolysis is added upstream of an anaerobic digester,biogas production is increased. However, this gain is countered by theenergy required for thermal hydrolysis. In more recent proposals,thermal hydrolysis is performed on dewatered digestate from a firststage digester. The hydrolysis product is diluted and sent to a secondstage digester. This provides an improvement in the energy balance. Theinventors believe, however, that the energy balance or resourcerecovery, or both, can be improved by minimizing or avoiding thedilution.

This specification describes a system and process in which digestatefrom a first digester is thickened or dewatered, hydrolysed and thentreated essentially without dilution in a high solids digester,optionally a mechanically mixed wet digester. A first stage digesteroptionally also operates at an elevated solids content, for example upto 8% or more DS in the digester. First stage digestate may optionallybe thickened or dewatered to 15% or more or 18% DS or more, for exampleabout 20% DS. The second stage digester operates at 7% or more, or 9% ormore, DS in the digester, optionally up to about 15% DS. Mixing isenabled by the use of mechanical mixers in at least the second stagedigester. Ammonia inhibition is avoided by withdrawing a liquid fractionof the first stage digestate from the system.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 shows a process flow diagram of a waste sludge treatment system.

DETAILED DESCRIPTION

FIG. 1 shows a sludge treatment system 10. The system 10 may be used,for example, to treat sludge 12 from a municipal wastewater treatmentplant (WWTP) (not shown). The sludge may include primary sludge, wasteactivated sludge, or both. The sludge 12, or part of it, may have beenpre-thickened in the wastewater treatment plant, for example up to asludge 12 solids content of about 4-6% DS.

The system 10 includes a first anaerobic digester 14 and a secondanaerobic digester 16. The digesters 14, 16 are configured in series.The digesters 14, 16 are, generally speaking, covered tanks with mixers.In the case of an existing WWTP, there may already be a digester tank,or two digester tanks configured in parallel, operated with hydraulicand solids retention times of about 20 days. These tanks might besuitable to be converted for use in the system 10. Alternatively, one ormore new digesters may be constructed.

Digester operation in the system 10 is preferably with a low hydraulicretention time, for example 6-12 days or 8-10 days, in the downstreamdigester 16 or both digesters 14, 16. The solids content in thedigesters 14, 16 is higher than in a typical WWTP. For example, thesecond digester 16 may operate at 7% DS or more, for example about 10%DS, in the digester. The first digester may operate at about 3-8% DS orin the digester, for example 5-8% DS. The solids content in the seconddigester 16, and possibly also in the first digester 14, is too high forconventional gas mixing. The second digester 16, and optionally thefirst digester 14, are mixed with hydraulic or electrical mixers, forexample as sold under the OMNIVORE trade mark by Anaergia.

A first digestate 18 is drawn from the first digester 14. Although theterm digestate is sometimes used to refer specifically to the solidsfraction in digested sludge, in this document “digestate” refers to thesludge removed from a digester unless indicated otherwise. The firstdigestate 18 is dewatered in dewatering unit 20. Dewatering unit 20 maybe, for example, a screw dewaterer having a tapered auger inside of acylindrical screen. Alternatively, a high solids content producingsludge thickener may be used.

The dewatering unit 20 produces a liquid fraction 22 and a solidfraction 24. The liquid fraction 22 contains ammonia and is preferablytreated to extract the ammonia, for example by passing the liquidfraction through an ammonia stripper. The extracted ammonia can beprocessed to produce, for example, ammonium hydroxide or ammoniumsulfate, which are useful in making fertilizer. The ammonia depletedliquid fraction 22 can optionally be treated for further resourcerecovery (for example of phosphorous) before being returned to the headof the WWTP.

Optionally, a portion of the solid fraction 24 may be recycled to thefirst digester 14. This provides recuperative thickening of the digester14 thereby increasing the solids content in the digester 14 and itssolids retention time. In another option (which may be used instead ofor in combination with recuperative thickening) a high solids thickener26 (for example a screw thickener) is added upstream of the firstdigester. The thickener 26 may increase the solids content of sludge 12to 8% DS or more or 10% DS or more, for example, 10-16% DS. Thethickener 26 may be, for example, a belt or screw thickener. A suitablescrew thickener is shown in International Publication Number WO2013/155630 A1, Sludge Screw Thickener with Screen Rotation DuringCleaning, by Anaergia Inc., which is incorporated herein by reference.In another option, the first digester 14 may receive sludge 12 at 2-6%DS solids, although the sludge 12 is preferably at least thickened to4-6% DS using conventional low solids thickening equipmentconventionally used in a WWTP. The first digester 14 optionally operatesat a solids content of 3-8% DS or more, for example 3-8% DS. Thehydraulic retention time in the first digester 14 is optionally 6-12 or8-10 days.

The solid fraction 24 may have a solids content of at least 15%. At thissolids content, some high solids thickeners may be useful in place ofdewatering unit 20. However, it is preferable for solid fraction 24 tohave a higher solids content, for example at least 16% or at least 18%or at least 20%, for example about 20%.

The solid fraction 24 is treated in a hydrolysis unit 28. In someexamples, the hydrolysis unit 28 may be a thermal hydrolysis unit thatuses heat, and optionally pressure, to treat the solid fraction 24.Commercial hydrolysis units are available, for example, from Cambi,Veolia, Lystek and OpenCell. The hydrolysis unit 28 hydrolyses largemolecules remaining in the solid fraction 24. Since treatment in thefirst digester 14 is conducted at a low solids residence time, forexample about 8-10 days, at least some of the solids are not completelydigested before hydrolysis. The hydrolysis unit 28 completes hydrolysisand may also lyse some cells in the solid fraction 24.

The hydrolysed solids fraction 24 is treated in second digester 16. Thehydrolysed solids fraction 25 is preferably not substantially diluted(or diluted at all), but sent to the second digester at a high solidscontent, for example 15% or more, 16% or more, 18% or more, or 20% ormore, for example about 20%. The second digester 16 may operate at 7% DSor more, or 9% DS or more, solids in the digester. This is enabled byusing mechanical, rather than air, mixers in digester 16. Mechanicalmixers may use a spinning blade or other moving solid object in contactwith the digestate to stir or otherwise mix the digestate in thedigester tank. A suitable digester 20 and mixers are available from UTSor Anaergia, for example as sold under the OMNIVORE trade mark.Hydraulic residence time in the second digester 16 is optionally about8-10 days.

High torque, low speed submersible mixers in at least the seconddigester 16, and optionally the first digester 14, are preferred. UTSProducts GmbH in Lippetal, Germany manufactures high solids contentsubmersible mixers 70 driven by a hydraulic motor, also availablethrough the related company UTS Biogas Ltd., Cambridgeshire, UK, andAnaergia Services in the US under the OMNIVORE trade mark. Each mixeruses a 22 kW external hydraulic power unit and circulates biodegradablehydraulic oil, such that if leaks occur inside the digester then thebacteria can degrade the non-toxic leaked oil. Usually two or moremixers are needed per digester tank, depending on the digester tankdimensions. Alternatively, UTS electrical mixers with a permanent magnetsynchronous motor may be used. These mixers are described in Germanpatent application 10 2014 116 239.0 entitled “Verfahren zum Betreibeneiner Ruhreinrichtung and eines Fermenters” filed on Nov. 7, 2014 whichis incorporated herein by reference. These mixers are able to mixdigestate at 7%, 8%, 9% and even 10% or more TS. Use of an air mixerwould require dilution of solids fraction 24 but this would preventrecovery of ammonia, in some cases encourage ammonia inhibition indigester 16, and result in less efficiency, or larger tank size, ofdigester 16.

The preferred digestate dewatering equipment is an enclosed rotary screwthickener with an internal screw, which is designed to thicken sludgewith a high initial solids content. Alternatively, to handle eventhicker digestate, the digestate 18 may be dewatered in two stages. Thefirst stage is performed without polymer, for example in a screwthickener. In the second stage, the filtrate (liquid fraction) from thefirst stage is treated with polymer, for example in a centrifuge orscrew thickener with smaller screen openings.

A digester operating at high solids content would normally be subject toammonia inhibition. However, removing liquid fraction 22 also lowers theammonia concentration in second digester 16. If the ammoniaconcentration in the second digester 16 exceeds potential inhibitionlevels, for example 5000-5500 mg/L, despite removal of liquid fraction22, micronutrients, for example a source of volatile carbon to increasethe C:N ratio, are added to the second digester 16.

U.S. Pat. No. 9,181,120 and US Publication 2012145627 and U.S.provisional application 62/265,691 filed on Dec. 10, 2015 areincorporated by reference.

Unless stated otherwise or apparent from the context, solids contents orconcentrations mentioned above are dried solids (DS) measurements whichwould be the same as a total solids (TS) measurement. In digestate, theDS is roughly 10% higher than total suspended solids (TSS) and the totaldissolved solids (TDS) is typically 2500 to 4000 mg/L (0.25 to 0.4%).For example, a 5% DS digestate may have 46,000 mg/L of TSS and 4000 mg/LTDS. Accordingly, solids contents or concentrations, unless specifiedotherwise, can generally be interpreted as TSS without causing amaterial difference in the process.

The descriptions of processes and apparatus above are to provide atleast one example of an embodiment within each claim but not to limit ordefine any claim. However, multiple processes and apparatus have beendescribed above and it is possible that a particular process orapparatus described above is not within a specific claim. Processparameters are given as examples of how a plant may be operated and arenot meant to limit a claim unless explicitly recited in a claim. Otherprocesses for similar applications might operate at parameters withinranges that are 50% or 100% larger in both directions than the parameterranges described above, or within a 50% or 100% variation from a singleparameter described above. If one or more elements or steps describedabove are used to treat other wastes or under other conditions, then oneor more process ranges described above might not be suitable and wouldbe substituted with other appropriate parameters. Various sub sets ofthe unit processes described in relation to plant 100 can be used inother treatment plants. Various sub sets of unit processes in thetreatment plants described above may also be combined in ways other thanthose described to produce different treatment plants. The descriptionof one process or apparatus may be useful in understanding anotherprocess or apparatus. Words such as “may”, “preferable” or “typical”, orvariations of them in the description above, indicate that a processstep or apparatus element is possible, preferable or typical, accordingto the word used, but still optional and not necessarily part of anyclaimed invention unless explicitly included in a claim.

We claim:
 1. A process for treating wastewater treatment plant (WWTP) orother sludge comprising the steps of, feeding the WWTP or other sludgeto an anaerobic digester; thickening or dewatering digestate from thefirst anaerobic digester; hydrolysing a first portion of the thickenedor dewatered digestate; returning a second portion of the thickened ordewater digestate to the anaerobic digester.
 2. The process of claim 1comprising feeding the hydrolysis product at 15% DS or more to a secondanaerobic digester.
 3. The process of claim 1 comprising feeding thehydrolysis product at 18% DS or more to a second anaerobic digester. 4.The process of claim 1 comprising feeding the hydrolysis product at 20%DS or more to a second anaerobic digester.
 5. The process of claim 1comprising producing a liquid fraction of the digestate from the firstanaerobic digester while thickening or dewatering the digestate from thefirst anaerobic digester and removing ammonia from the liquid fractionto produce an ammonia depleted liquid fraction.
 6. The process of claim5 wherein the sludge is from a WWTP and the ammonia depleted liquidfraction is returned to the WWTP.
 7. The process of claim 1 comprisingstirring the second anaerobic digester with an electric or hydraulicpowered mixer.
 8. The process of claim 1 comprising operating theanaerobic digester at 3-8% DS.
 9. A system for treating WWTP or othersludges comprising, an anaerobic digester; a sludge thickener ordewaterer downstream of the anaerobic digester; and, a hydrolysis unitdownstream of the anaerobic digester, a recycle loop from between thesludge thickener or dewaterer and the hydrolysis unit to the anaerobicdigester.
 10. The system of claim 9 wherein the sludge thickener ordewaterer has a solids fraction outlet and a liquid fraction outlet, andthe liquid fraction outlet is connected to a WWTP.
 11. The system ofclaim 9 comprising a second anaerobic digester downstream of thehydrolysis loop.